Apparatus for catalytic treatment of hydrocarbons



Aug. '1, 1950 E. M. BARBER APPARATUS Foa CATALYTIG TREATMENT oF HYDRocARBoNs Filed June 14, 1947 INVENTOR. EVE/ 25 TTM. BA /PE/Q Patented Aug. 1, 1%950 A'PPRAIUS` FR CATALYTIC TREATMENT."

. DFHYDROCARBONS .Everett M; Barber,Wappingers Falls, N. Y., as-

isignorfto ThezTexas Company, New York, N. Y., atcorporation of Delaware f Application ceneri, 1947, serialivazsam larly `adapted for processes 1in which the 'catalyst is lregenerated in which case the catalyst beds are moved through the elongated chamber through transverse 'streams o'f *hydrocarbons for process- `ing and `regeneratinggas for reactivating-the catalyst.

The invention contemplates an elongated chamber `containing -a plurality ofvcata'lyst beds disposed for translation Ltherein and=ports in the chamber to provide `for the passage of fluids through the catalyst transverselyto the path of movement of the beds. In accordance @with the invention the `cl-iamber is Aprovided with means P for introducing spacer elements 'and catalyst at one end thereof `to "thereby charge segregated bodies of `catalyst to thel chamber, means for positively moving the *segregated increments `of catalyst through the `chamber and means `for introducing hydrocarbons and regenerating vgas to spaced zone'sin thechamber for transverse 'flow through *the severalucatalyst beds.

The invention *particularly directed to the catalytic cracking "of hydrocarbonfoil and fis especially adaptedffor obtaining-good conversions with "Thigh roil to 'catalyst jratios for "high specific through-puts and with `reduced #equipment sizes and catalyst inventories; l

The invention Ibe understood trom 4the ifdllowing detailed description` fthereof having reference to theraccompanying drawings wherein:

Fig. V1 is a longitudinal section of an elongated reactor constituting afpreferred embodiment of the invention.

Fig. 3 is an enlarged perspective view of a "dual spacer disk adapted to"Aj avel within the reactor.

As shown in thedrawi'rig an"elongate`d cylin- 'i drical `chairiher vor pipe `AIl) iisfarranged f-or the `passage Vof the catalyst through the 'pipe through successive regenerating, processing and jpurgi-n'g sections thereof. nt the chargingwend ofi ithepipe la `pepper in is opposes: for `nuroclaein,J cannet .2.;Claims. (01.23-288) its into the pipe reactor ID. Immediately ahead `of the hopper there is `an opening l E in the pipe for the insertion of metal spacer disks i3. Asshown in Fig. 3, the spacer disk-s are preferably in the form of a spool `comprising a pair of disks interconnected by an axial rod. Each disk is of a diameter adapted to provide a neat running fit within the pipe reactor. These .spacer elements may be in the form of `a single disk but the dual :form is preferable since it facilitates the proper translation of the disks Within the .pipe,

A piston M operated by a thrustor actuator l 5 is disposed at .the charging end of the pipe reactor. The piston is shown in the drawing in a partially retracted position. With the piston in the completely retracted position a spoolvl3 is inserted throughthe opening l2. Upon the forward movenient of 'the piston, `the spool is pushed forward beneath the hopper, the forward disk or the spool being moved just past spring-pressed triggers 1'6. The space between the dual disks is filled with .catalyst from vthe hopper, the catalyst received from the hopper being collected as a 'compact mass -or bed within the dualidisks. When thepiston is again retracted, another spool iS inserted through the opening I2 and the latter spool fis pushed forward to replace the one under the hopper. In `this Way, the .several spools containing the several increments of catalyst are pushed Aforward through the pipe reactor through successive regenerating, purging `and processing sections thereof. l

In the regenerating section air or oxygen-containing gas is 'introduced through a pipe llinto za `chamber 18 which surmounts the pipe reactor. The oxygen-containing gas flows from this cham- Aber through a plurality of ports I9 thence `'through the mass of catalyst. "The products of combustion are discharged through outlet ports .Mlinto a receiving chamber 2| from which the gaseous products areremove'd through a line 22.

In the succeeding purging `section a gas such as ilue gas or 'steam is `directed through a line 23 into a `chamber 24 from which the purging :gas is passed through a plurality of ports 2d into the catalyst mass so as to `remove therefrom any products of combustion remaining after the regenerating step. The eliluent gases flow through a yplurality of ports 26 into` a receiving chamber "2l and are removed through a pipe 28.

vInthe processing section hydrocarbons to be subjected to the catalytic treatment :are intro-j 'duced through a pipe 279 into aldistributingchamber' 30 and pass thence through aplurality ol ports T31 through fthe catalyst mass. -Theproducts of reaction flow through a plurality of ports 32 into a receiving chamber 33 and are removed through a line 34 to suitable fractionating equipment for recovering the products.

In a preferred embodiment of the invention a centrifugal blower 35 is mounted in the chamber 30. In operating `with the blower the hydrocarbon oil is preheated to a temperature just below the thermal cracking temperature and introduced at such temperature through the pipe 29. The rise in temperature from the compression produced by the blower functions to immediately raise the temperature of the oil to the temperature desired for the catalytic cracking, The time element under the compression prior to contacting with the catalyst is so small that any thermal cracking effect is practically eliminated.

In the succeeding purging section a suitable medium such as steam or inert gas, adapted for removing any hydrocarbons which may be contained in the catalyst after processing, is directed. through a line 30 into a chamber 3l. The purging medium flows through a plurality of ports 38 thence into the catalyst mass. The efuent gases pass through a plurality of ports 39 into a receiving chamber 40 and are removed through a line 4l.

In each of the several processing, regenerating and purging zones, the assemblies of inlet and outlet ports are disposed opposite each other so as to establish a current of fluid owing through the catalyst mass transversely of the path of movement of the catalyst beds. Preferably, these ports. are arranged at the top and bottom of the elongated cylindrical chamber I0 so as to provide ver-- tical paths of now, downwardly or upwardly, through the catalyst beds. The hydrocarbons to be processed and the reactivating and purging gases are passed in continuous streams and catalyst beds are moved successively across the paths of the several streams. Although in the specic: `description herein the hydrocarbons and the regenerating gas are indicated as flowing in the same direction an advantageous operation is to have the flow of fluids in the processing and regenerating zones in opposite directions.

As shown in the drawing, screens 42 may be provided about the several assemblies of ports i9, .20, 25, 26, 3l, 32, 38 and 3S. While the screens are not always necessary, it is desirable t0 use them particularly when operating with the ner grades of catalyst in order to prevent loss of catalyst through the ports in the pipe reactor.

In practicing the invention for the cracking of oil any of the usual solid catalysts which are used in the cracking of hydrocarbons may be employed such as natural or synthetic composites of silica and alumina. Various composites of precipitated silica and alumina are well known as superior cracking catalysts. The catalyst is used in granular or pulverulent form, in pellets, in beads and the like.

The catalyst received from the charging hopper is collected in segregated compact masses within the several spools and the several increments of catalyst are forced through the pipe reactor through the successive regenerating, processing and purging sections thereof. The hydrocarbons in the processing zone, the reactivating gases in the regenerating zone and the purging gases in the purging zones now through the several increments of moving catalyst transversely to the path of movement of the catalyst. The

of oil per hour per volume of catalyst, is regulated by the rate at which the hydrocarbons are charged to the processing section and the rate at which the catalyst is moved through the processing section. The time element in the processing, regenerating and purging zones is controlled by the axial length of the several Zones and the rate at which, the catalyst is passed therethrough." The movement of the piston is timed in accordance with the operating cycle desired. In the drawing the axial length of the processing section is indicated to be somewhat longer than that of the regenerating section; the relative length of these two sections will, however, vary with the character of the charging stock used and the amount of deposition of coke or carbon on the catalyst. Frequently it will be found that the axial length of the regenerating section should be greater than that of the processing section.

Each of the axial lengths, B, C and D should be of materially greater length than the diameter of the pipe reactor in order to assure that the iluids flowing through the several regenerating, purging and processing sections will not iiow from one of these sections to an adjacent section. Similarly the axial lengths A and E should be materially greater than the diameter of the pipe reactor so as to 'assure that gaseous or vaporous constit.- uents will not pass out through the charging or discharging ends of the pipe reactor. Itisladvisable to maintain the pressures in the several processing, regenerating and-purging zones approximately the same so as to minimize the possibility of the now of gases from one zone to another.A Y

The used catalyst and the spaced disks are discharged from the pipe. reactor vto a conveyor 43. By means of the conveyor the used catalyst and the spacer disks may be returned to the charging end of the pipe reactor. Fresh or make-up catalyst is added to the hopper l l as needed and the mixture of fresh and used catalyst isA charged to the system. l

In the particular arrangement illustrated in thevdrawing a sequence of regeneration followed by processing is shown. This is an advantageous sequence when the used catalyst is subjected to vregeneration since it enables the bringing of highly heated catalyst to the processing stage.

The invention contemplates,y however, that the sequence may be reversed, the catalyst rst passing through a processing stage and then to a regeneratingl stage. In cases where it is not desired to reactivate the catalyst the regenerating stage may be omitted, the catalyst being charged directly to the processing stage and after going through a purging stage, delivered to the conveyor for removal of the catalyst from the system. In cases where noregenerating stage is employed or where the sequence is processing followed by regeneration, it is advantageous to provide ahead of the processing stage,.a -preheating stage in which the catalyst may be heated for delivery tothe processing stage. l

In the catalytic cracking of hydrocarbon oil, in accordance with thelinvention, theoil is'preheated to the desired temperature ofx reaction or to aV temperature approaching such temperature and directed throughthe inlet 29 for passage through the catalyst. Ingeneral, the temperatures applied in catalytic cracking are upwards of 850"v F. including temperatures of the lorder of 900 F. and l000` F. The operation-is conducted at atmospheric pressure or at moderate super-atmospheric pressures such a. around 5 50 lbs. pressure, since the low pressures are more satisfactory in catalytic cracking than high pressures. The invention facilitates operations with high space velocities and short cycles of processing and regenerating.

Although a preferred embodiment of the invention has been described herein, it will be understood that various changes and modifications may be made therein, while securing to a greater or less extent some or all of the benefits of the invention, without departing` from the spirit and scope thereof.

I claim:

1. In apparatus for the catalytic treatment oi' hydrocarbons, an elongated cylindrical chamber, a. plurality of retaining elements adapted for the segregation of beds of pulverulent catalyst and adapted for translation within the chamber, an opening at one end of the chamber adapted for the insertion of said retaining elements individually in seriatim, a hopper adapted to charge pulverulent catalyst into the chamber, a power actuated piston so disposed at said end of the chamber that upon retraction said opening is exposed for the insertion of a retaining element chamber by the translation of the retaining elements.

2. In apparatus for the catalytic treatment of hydrocarbons, an elongated cylindrical chamber, a plurality of spools adapted for translation Within the chamber, an opening at one end of the chamber adapted for the insertion of the spools individually in seriatim, a hopper adapted to charge pulverulent catalyst intothe chamber, a power actuated piston so disposed at said end of the chamber that upon retraction said opening is exposed for the insertion of a spool and upon the forward movement the inserted spool is pushed beneath the hopper and inflow and outow ports in a succeeding portion of the chamber disposed to provide transverse flow of fluids thru the several increments of catalyst as moved thru the chamber by the translation of the spools.

EVEREIT M. BARBER.

REFERENCES CITED The following references are of record in the le of this patent:

UNITED STATES PATENTS Number Name Date 1,048,019 Wilson Dec. 24, 1912 2,304,397 Campbell Deo. 8, 1942 2,327,438 Kuhn Aug, 24, 1943 

1. IN APPARATUS FOR THE CATALYTIC TREATMENT OF HYDROCARBONS, AN ELONGATED CYLINDRICAL CHAMBER A PLURALITY OF RETAINING ELEMENTS ADAPTED FOR THE SEGREGATION OF BEDS OF PULVERULENT CATALYST AND ADAPTED FOR TRANSLATION WITHIN THE CHAMBER, AN OPEINING AT ONE END OF THE CHAMBER ADAPTED FOR THE INSERTION OF SAID RETAINING ELEMENTS INDIVIDUALLY IN SERIATIM, A HOPPER ADAPTED TO CHARGE PURVERULENT CATALYST INTO THE CHAMBER, A POWER ACTUATED PISTON SO DIPOSED AT SAID END OF THE CHAMBER THAT UPON RETRACTION SAID OPENING IS EX- 